CN217961351U - Butanol and octanol production heat energy coupled system - Google Patents
Butanol and octanol production heat energy coupled system Download PDFInfo
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- CN217961351U CN217961351U CN202222356561.8U CN202222356561U CN217961351U CN 217961351 U CN217961351 U CN 217961351U CN 202222356561 U CN202222356561 U CN 202222356561U CN 217961351 U CN217961351 U CN 217961351U
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Abstract
The utility model relates to a butyl octanol production heat energy coupled system, include: a butyraldehyde separation tower, an isobutanol tower and an n-butanol tower. The tower bottom of the butyraldehyde separation tower is provided with a butyraldehyde separation tower steam reboiler and a butyraldehyde separation tower heat exchange reboiler; the tower bottom of the isobutanol tower is provided with an isobutanol tower steam reboiler and an isobutanol tower heat exchange reboiler, and the tower top gas phase outlet of the isobutanol tower is connected to the heat exchange medium inlet of the butyraldehyde separation tower heat exchange reboiler; and a side inlet of the n-butanol tower is connected with a tower bottom liquid phase extraction outlet of the isobutanol tower, and a tower top gas phase outlet pipeline of the n-butanol tower is connected to a heat exchange medium inlet of the isobutanol tower heat exchange reboiler. The utility model discloses a triple effect thermal coupling regards isobutanol top of the tower gas phase part as the heat source of butyraldehyde knockout tower reboiler, and isobutanol top of the tower gas phase reduces the use amount of steam and cooling water, reduction production energy consumption as the heat source of isobutanol tower reboiler by a wide margin.
Description
Technical Field
The utility model belongs to the chemical industry field relates to butyl octanol production technology, especially a butyl octanol production heat energy coupled system.
Background
With the development of petrochemical industry, polyvinyl chloride plastic industry and organic chemical industry, the industry of butanol and octanol is rapidly developed, and main products of the industry, namely the butanol, the isobutanol and the octanol, are important fine chemical raw materials and are widely applied to the fields of chemical industry, medicines, coatings and the like.
The industrial production method of butanol and octanol mainly includes acetaldehyde condensation method, fermentation method, ziegler method and oxo synthesis method, etc., and the former three methods have the disadvantages of limited raw material source, high energy consumption and high production cost. The propylene oxo synthesis method has gradually become the most important technical route for producing butanol and octanol in the world.
The butanol-octanol carbonyl synthesis process uses propylene, synthesis gas and hydrogen as raw materials, mixed butyraldehyde is generated under the action of a catalyst, the catalyst is separated for recycling, n-butyl alcohol and isobutanol are generated by separating n-butyraldehyde/isobutyraldehyde through hydrogenation, and n-butyl alcohol and isobutanol products are obtained through rectification separation: the n-butyl aldehyde is subjected to condensation reaction under the action of an alkali catalyst to generate octenal, the octenal is hydrogenated to produce crude octanol, and the crude octanol is rectified to obtain the product octanol.
At present, an isomerate tower is arranged for completely separating n-butyraldehyde and isobutyraldehyde produced by a domestic butanol and octanol device, a reboiler is arranged at a tower kettle of the isomerate tower, steam is used as a heat source at the tower kettle, and the steam required for separating the n-butyraldehyde and the isobutyraldehyde is provided through the reboiler.
In the hydrogenation working section of the butanol-octanol device, n-butyraldehyde is hydrogenated to generate crude butanol, and two rectifying towers, namely a light removal tower and a heavy removal tower, are arranged to complete the separation work of high-purity n-butanol. The tower kettle of the heavy component removal tower is provided with a reboiler, the tower top is provided with a condenser, the gas phase temperature at the tower top is 130-140 ℃, more circulating water is consumed when the gas phase at the tower top is condensed, and the comprehensive energy consumption is high.
CN104788302A discloses a separation and purification system and a separation and purification method for n-butyraldehyde and isobutyraldehyde, and the designed systems are independent, and do not utilize the heat of materials, so that the equipment is more, the energy consumption is high, and the investment cost is high.
SUMMERY OF THE UTILITY MODEL
The utility model aims to overcome prior art's weak point, provide a butyl octanol production heat energy coupled system, reduce the energy consumption of butyl octanol production by a wide margin.
The utility model provides a technical scheme that technical problem adopted is:
a butanol-octanol production heat energy coupling system, comprising: a butyraldehyde separation tower, an isobutanol tower and an n-butanol tower. The tower bottom of the butyraldehyde separation tower is provided with a butyraldehyde separation tower steam reboiler and a butyraldehyde separation tower heat exchange reboiler; the tower bottom of the isobutanol tower is provided with an isobutanol tower steam reboiler and an isobutanol tower heat exchange reboiler, and the tower top gas phase outlet of the isobutanol tower is connected to the heat exchange medium inlet of the butyraldehyde separation tower heat exchange reboiler; and a side inlet of the n-butanol tower is connected with a tower bottom liquid phase extraction outlet of the isobutanol tower, and a tower top gas phase outlet pipeline of the n-butanol tower is connected to a heat exchange medium inlet of the isobutanol tower heat exchange reboiler.
Further, a gas phase outlet pipeline at the top of the isobutanol tower is divided into two paths, one path is connected to a heat exchange medium inlet of the butyraldehyde separation tower heat exchange reboiler, the other path is connected to an inlet of an isobutanol tower condenser, an outlet pipeline of the isobutanol tower condenser is connected to an inlet of an isobutanol tower reflux tank, and an outlet pipeline of the isobutanol tower reflux tank is connected to a top reflux port of the isobutanol tower.
Further, a heat exchange medium outlet pipeline of the heat exchange reboiler of the butyraldehyde separation tower is connected to an inlet of a reflux tank of the isobutanol tower.
Further, an outlet pipeline of a heat exchange medium of the isobutanol tower heat exchange reboiler is connected to an inlet of a n-butanol tower reflux tank, and an outlet pipeline of the n-butanol tower reflux tank is connected to a tower top reflux port of the n-butanol tower.
Furthermore, an n-butanol tower reboiler is arranged at the bottom of the n-butanol tower.
Further, an outlet of the tower top of the butyraldehyde separation tower is connected with an inlet of a condenser of the butyraldehyde separation tower, an outlet of the condenser of the butyraldehyde separation tower is connected with an inlet of a reflux tank of the butyraldehyde separation tower, and an oil phase outlet pipeline of the reflux tank of the butyraldehyde separation tower is connected with a tower top reflux port of the butyraldehyde separation tower through a pump.
The utility model discloses an advantage is with positive effect:
the utility model discloses a triple effect thermal coupling regards isobutanol top of the tower gas phase part as the heat source of butyraldehyde knockout tower reboiler, and the heat source of isobutanol tower reboiler is regarded as to n-butyl alcohol top of the tower gas phase, reduces the use amount of steam and cooling water by a wide margin, reduces the production energy consumption.
Drawings
Figure 1 is according to the utility model discloses butanol octanol production heat energy coupling system diagram.
A 1-butyraldehyde separation column; a 2-butyraldehyde separation tower steam reboiler; a heat exchange reboiler of the 3-butyraldehyde separation tower; a 4-butyraldehyde separation tower condenser; a reflux tank of a 5-butyraldehyde separation tower; a 6-isobutanol column; a 7-isobutanol column steam reboiler; 8-isobutanol tower heat exchange reboiler; a 9-isobutanol column condenser; a 10-isobutanol column reflux tank; 11-n-butanol column; 12-n-butanol column reboiler; 13-n-butanol column reflux drum.
Detailed Description
It should be noted that, in the present application, the embodiments and features of the embodiments may be combined with each other without conflict. The present invention will be described in detail below with reference to the accompanying drawings in conjunction with embodiments.
It is noted that, unless otherwise indicated, all technical and scientific terms used herein have the same meaning as commonly understood by one of ordinary skill in the art to which this application belongs.
The butanol and octanol production process comprises a butyraldehyde separation section, a butyraldehyde reaction section for generating butanol, and a butanol refining section, wherein a butyraldehyde separation tower, an isobutanol tower and an n-butanol tower are provided with a separate condenser and a reboiler in front, and the consumption of steam and the cooling water amount are high.
The scheme adopts three-effect thermal coupling, the gas phase part at the top of the isobutanol tower is used as a heat source of a butyraldehyde separation tower reboiler, and the gas phase at the top of the n-butanol tower is used as a heat source of an isobutanol tower reboiler, so that the use amount of steam and cooling water is greatly reduced, and the production energy consumption is reduced.
The utility model discloses a butyl octanol production heat energy coupled system, include: butyraldehyde separation tower 1, isobutanol tower 6 and n-butanol tower 11.
A butyraldehyde separation tower steam reboiler 2 and a butyraldehyde separation tower heat exchange reboiler 3 are arranged at the tower bottom of the butyraldehyde separation tower 1, an outlet at the tower top of the butyraldehyde separation tower 1 is connected with an inlet of a butyraldehyde separation tower condenser 4, an outlet of the butyraldehyde separation tower condenser 4 is connected with an inlet of a butyraldehyde separation tower reflux tank 5, and an oil phase outlet pipeline of the butyraldehyde separation tower reflux tank 5 is connected with a tower top reflux port of the butyraldehyde separation tower 1 through a pump; and a water phase outlet pipeline of the butyraldehyde separation tower reflux tank 5 is connected to a waste water discharge device. The side surface of the butyraldehyde separation tower 1 is provided with a crude butyraldehyde raw material inlet and an isobutyraldehyde product outlet. And the tower kettle outlet of the butyraldehyde separation tower 1 is connected to a crude butyraldehyde reaction section through a pump.
The bottom of the isobutanol tower 6 is provided with an isobutanol tower steam reboiler 7 and an isobutanol tower heat exchange reboiler 8, the top gas phase outlet pipeline of the isobutanol tower 6 is divided into two paths, one path is connected to the heat exchange medium inlet of the isobutanol tower heat exchange reboiler 3, the other path is connected to the inlet of an isobutanol tower condenser 9, the outlet pipeline of the isobutanol tower condenser 9 is connected to the first inlet of an isobutanol tower reflux tank 10, the outlet pipeline of the isobutanol tower reflux tank 10 is divided into two paths through a pump, one path is used as an isobutanol product extraction pipeline, the other path is connected to the top reflux port of the isobutanol tower 6, and the heat exchange medium outlet pipeline of the isobutanol tower heat exchange reboiler 3 is connected to the second inlet of the isobutanol tower reflux tank 10. The side of the isobutanol column 6 has a crude butanol inlet.
The side surface inlet of the n-butanol tower 11 is connected with the tower bottom liquid phase extraction outlet of the isobutanol tower 6, the bottom of the n-butanol tower 11 is provided with an n-butanol tower reboiler 12, the top gas phase outlet pipeline of the n-butanol tower 11 is connected to the heat exchange medium inlet of the isobutanol tower heat exchange reboiler 8, the heat exchange medium outlet pipeline of the isobutanol tower heat exchange reboiler 8 is connected to the inlet of an n-butanol tower reflux tank 13, the outlet pipeline of the n-butanol tower reflux tank 13 is divided into two paths, one path is connected to the top reflux port of the n-butanol tower 11, and the other path is an n-butanol product extraction pipeline.
The process method of the system comprises the following steps:
the method comprises the following steps of removing light components from crude butyraldehyde, feeding the crude butyraldehyde into a butyraldehyde separation tower 1, wherein the butyraldehyde separation tower 1 is provided with two reboilers, one is a steam reboiler 2 of the butyraldehyde separation tower, steam is used as a heat source and is used as a standby reboiler, the other is a heat exchange reboiler 3 of the butyraldehyde separation tower, the gas phase at the top of an isobutyraldehyde tower is used as a heat source, the pressure at the top of the butyraldehyde separation tower is 60-70kPa, the temperature at the top of the tower is 40-50 ℃, the temperature at a tower kettle is 60-70 ℃, the gas phase at the top of the butyraldehyde separation tower 1 enters a condenser 4 of the butyraldehyde separation tower, condensed liquid enters a reflux tank 5 of the butyraldehyde separation tower and is subjected to phase splitting in the tank, the water phase is a wastewater discharge device, an oil phase is used as a reflux pump and returns to the butyraldehyde separation tower 1, an isobutyraldehyde product is collected from the lateral line of the butyraldehyde separation tower kettle, and is used as a crude butyraldehyde to be sent to a reaction section. The crude butyraldehyde is converted into crude butanol through a reaction section, the crude butanol enters an isobutanol tower 6 after light components are removed from the crude butanol, the isobutanol tower 6 is provided with two reboilers, one is an isobutanol tower steam reboiler 7, steam is used as a heat source, the other is an isobutanol tower heat exchange reboiler 8, and the gas phase at the top of an n-butanol tower 11 is used as a heat source; the pressure of the top of the tower is 40-50kPa, the temperature of the top of the tower is 80-90 ℃, the temperature of the bottom of the tower is 100-110 ℃, the gas phase part of the top of the isobutyl alcohol tower 6 enters a butyraldehyde separation tower heat exchange reboiler 3, part of the gas phase part enters an isobutyl alcohol tower condenser 9, the condensed gas phase part enters an isobutyl alcohol tower reflux tank 10, the liquid part in the tank reflows and is extracted as an isobutyl alcohol product, the liquid phase part of the bottom of the isobutyl alcohol tower 6 enters an n-butyl alcohol tower 11, the pressure of the top of the tower is 160-170kPa, the temperature of the top of the tower is 130-140, the temperature of the bottom of the tower is 135-145 ℃, the gas phase part of the top of the n-butyl alcohol tower 11 enters an isobutyl alcohol tower heat exchange reboiler 8, the condensed gas phase part enters an n-butyl alcohol tower reflux tank 13, and the liquid part in the tank reflows and is extracted as an n-butyl alcohol product. Heavy components are extracted from the liquid phase at the bottom of the n-butanol tower 11.
The above description is only a preferred embodiment of the present invention and is not intended to limit the present invention, and various modifications and changes may be made by those skilled in the art. Any modification, equivalent replacement, or improvement made within the spirit and principle of the present invention should be included in the protection scope of the present invention.
Claims (6)
1. A butanol octanol production heat energy coupled system, its characterized in that includes:
the tower bottom of the butyraldehyde separation tower (1) is provided with a butyraldehyde separation tower steam reboiler (2) and a butyraldehyde separation tower heat exchange reboiler (3);
the device comprises an isobutanol tower (6), wherein an isobutanol tower steam reboiler (7) and an isobutanol tower heat exchange reboiler (8) are arranged at the bottom of the isobutanol tower (6), and a gas phase outlet at the top of the isobutanol tower (6) is connected to a heat exchange medium inlet of the butyraldehyde separation tower heat exchange reboiler (3);
the side inlet of the n-butanol tower (11) is connected with the tower bottom liquid phase extraction outlet of the iso-butanol tower (6), and the tower top gas phase outlet pipeline of the n-butanol tower (11) is connected to the heat exchange medium inlet of the iso-butanol tower heat exchange reboiler (8).
2. The coupling system for coupling butanol-octanol production heat energy according to claim 1, wherein the top gas phase outlet line of the isobutanol column (6) is divided into two paths, one path is connected to the inlet of the heat exchange medium of the butyraldehyde separation column heat exchange reboiler (3), the other path is connected to the inlet of the isobutanol column condenser (9), the outlet line of the isobutanol column condenser (9) is connected to the inlet of the isobutanol column reflux tank (10), and the outlet line of the isobutanol column reflux tank (10) is connected to the top reflux port of the isobutanol column (6).
3. The butanol-octanol production heat energy coupling system according to claim 2, wherein the heat exchange medium outlet pipeline of butyraldehyde separation column heat exchange reboiler (3) is connected to the inlet of isobutanol column reflux drum (10).
4. Butanol-octanol production heat energy coupling system according to claim 1, wherein the heat exchange medium outlet line of isobutanol column heat exchange reboiler (8) is connected to the inlet of n-butanol column reflux drum (13), and the outlet line of n-butanol column reflux drum (13) is connected to the top reflux inlet of n-butanol column (11).
5. Butanol-octanol production heat energy coupling system according to claim 4, wherein the bottom of the n-butanol column (11) is provided with an n-butanol column reboiler (12).
6. The butanol-octanol production heat energy coupling system according to claim 1, wherein the top outlet of the butyraldehyde separation tower (1) is connected to the inlet of a butyraldehyde separation tower condenser (4), the outlet of the butyraldehyde separation tower condenser (4) is connected to the inlet of a butyraldehyde separation tower reflux tank (5), and the oil phase outlet pipeline of the butyraldehyde separation tower reflux tank (5) is connected to the top reflux port of the butyraldehyde separation tower (1) through a pump.
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| Application Number | Priority Date | Filing Date | Title |
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| CN202222356561.8U CN217961351U (en) | 2022-09-06 | 2022-09-06 | Butanol and octanol production heat energy coupled system |
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| CN202222356561.8U CN217961351U (en) | 2022-09-06 | 2022-09-06 | Butanol and octanol production heat energy coupled system |
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